CA2121670C - Process and apparatus for distributing fluids in a container - Google Patents
Process and apparatus for distributing fluids in a container Download PDFInfo
- Publication number
- CA2121670C CA2121670C CA002121670A CA2121670A CA2121670C CA 2121670 C CA2121670 C CA 2121670C CA 002121670 A CA002121670 A CA 002121670A CA 2121670 A CA2121670 A CA 2121670A CA 2121670 C CA2121670 C CA 2121670C
- Authority
- CA
- Canada
- Prior art keywords
- fluid
- arms
- mass
- vessel
- inlet conduit
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000012530 fluid Substances 0.000 title claims abstract description 179
- 238000000034 method Methods 0.000 title abstract description 12
- 230000008569 process Effects 0.000 title abstract description 12
- 238000009826 distribution Methods 0.000 claims abstract description 44
- 238000012856 packing Methods 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 description 42
- 239000007787 solid Substances 0.000 description 19
- 239000007789 gas Substances 0.000 description 15
- 239000002245 particle Substances 0.000 description 10
- 238000004231 fluid catalytic cracking Methods 0.000 description 9
- 230000008901 benefit Effects 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 239000006185 dispersion Substances 0.000 description 5
- 238000004523 catalytic cracking Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 239000003575 carbonaceous material Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000003628 erosive effect Effects 0.000 description 3
- 230000003993 interaction Effects 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000000567 combustion gas Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000002829 reductive effect Effects 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000000670 limiting effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
- C10G11/182—Regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
- B65G—TRANSPORT OR STORAGE DEVICES, e.g. CONVEYORS FOR LOADING OR TIPPING, SHOP CONVEYOR SYSTEMS OR PNEUMATIC TUBE CONVEYORS
- B65G53/00—Conveying materials in bulk through troughs, pipes or tubes by floating the materials or by flow of gas, liquid or foam
- B65G53/34—Details
- B65G53/52—Adaptations of pipes or tubes
- B65G53/528—Flux combining or dividing arrangements
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Mechanical Engineering (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
Process for radial distribution of fluid into a fluid mass wherein fluid is radially conveyed within and isolated from the fluid mass and discharged via a plurality of distribution points located radially in the fluid mass.
Description
PROCESS AND APPARATUS FOR DISTRIBUTING
FLUIDS IN A CONTAINER
The present invention relates to a process for introducing a stream of fluid into a fluid mass to rapidly attain uniform radial fluid distribution, arid to an apparatus therefor.
More particularly, the invention relates to a process for introducing fluidized solid particles into a bed of fluidised solids particles, for example for introducing catalyst particles into a fluidized bed of catalyst particles such as is present in the regenerator or reactor of a fluid catalytic cracking (FCC) reactor to rapidly attain uniform radial distribution of introduced solids, and to an apparatus therefor.
Fluidized catalytic cracking processes operate by circulating catalyst particles continuously from a reactor in which a hydrocarbon feed is cracked to lower boiling products, during which cracking carbonaceous material is deposited on the catalyst, via a regenerator in which the carbonaceous material is combusted to restore the catalyst activity, and returning catalyst particles to the reactor. Temperature of combustion in the regenerator is locally dependent on the amount of carbonaceous material on the catalyst and the supply of combustion gas in a given region.
Whilst operation with a single catalyst inlet opening at the regenerator side wall has for many years been satisfactory, the benefit to be obtained by improving radial distribution in conventional processes has become apparent. The benefits available from improved distribution of catalyst are particularly apparent for units comprising a regenerator vessel of increased diameter or in which regeneration is conducted at relatively high temperatures.
Such is the case for example with the processing of residual feeds or where limited elevation space or specific operation mode require operation with a reduced regenerator fluid bed height, combined with a large bed diameter. A condition for optimum regeneration is that the time for radial mixing of catalyst be less than that for coke combustion. With relatively high regeneration temperatures and heavier feed processing the rate of coke combustion is increased, requiring decrease in radial mixing time. With increase in diameter of a fluid bed, catalyst distribution must be more effective to prevent corresponding increase in radial mixing time. Should this condition not be met, radial gradients of coke, combustion gas and temperature form within the bed leading to an increase in oxygen content of flue gas and afterburn and a decrease in coke burning capacity for a given air blower.
In US Patent No. 4,595,567, devices disclosed for distributing catalyst into an FCC regenerator bed, described as air/catalyst distribution grids, would seem to comprise a plurality of openings 1.5 along the length of sections of a radially extending grid.
In US Patent No. 4,150,090 a device is disclosed comprising an axially located transport riser projecting from the lower part of an FCC regenerator vessel and supporting a plurality of radially extending fluidised catalyst distributor troughs, located in downward sloping direction at the surface of a regenerator bed.
Catalyst is transported and expelled along the length of the open-top troughs by means of fluidising gas supplied via conduits running along the length of the troughs and having apertures along the length thereof.
In US Patent No. 5,156,817 devices are disclosed for supplying catalyst to one or a plurality of open-sided channels defined between a base and top member of, for instance, inverted v-shaped cross-section by which means catalyst is discharged along the length of the channel(s), the channels) being closed at their proximal end. A single channel forms an incomplete annulus in an FCC regenerator bed. A plurality of channels are of different lengths and emanate in a fan formation from a supply conduit located towards the side of the bed, the longest channel extending to the axis of the regenerator bed.
2121fi~0 These devices suffer from the disadvantage that with normal operation, catalyst discharge is uneven along the distribution length, i.e. the plural openings, troughs and channels respectively, occurring to a lesser extent at the remote ends of the distribution lengths. The performance may be improved by employing excessive pressure drop which could be detrimental to the pressure balance of the unit. Provision of aeration conduits along distribution troughs incur high installation and maintenance costs.
In the latter cases radial mixing is governed by interaction between the flow pattern in the channels or troughs and the fluidised bed, and is therefor sensitive to changes in flow rate in the distributor which may affect the quality of radial distribution.
We have now found that fluids introduction and subsequent mixing into a fluid mass can be attained in a simple and controllable manner which is moreover robust to changes in distributor fluid flow. This manner relies on discharging the fluid at specific points in the fluid mass whilst avoiding interaction between the bed and the fluid to be distributed until the discharge point is reached. It has surprisingly been found that by this manner radial catalyst distribution gradients in the fluid mass are rapidly dissipated which would not have been expected. At the fluid discharge point the fluid kinetic energy may be locally eliminated after which the normal mixing action of the fluid mass promotes further radial mixing.
Accordingly, the present invention provides a process for radial distribution of fluid in a fluid mass wherein fluid is radially conveyed within and isolated from the fluid mass and discharged via a plurality of distribution points located radially in the fluid mass.
Suitably fluid is conveyed along radial paths, each path leading to a single distribution point, which point may provide one or more sites for contact of conveyed fluid and the fluids mass.
In a preferred embodiment of the process according to the invention fluid is discharged at a distance at least one quarter of 2~21~~~
FLUIDS IN A CONTAINER
The present invention relates to a process for introducing a stream of fluid into a fluid mass to rapidly attain uniform radial fluid distribution, arid to an apparatus therefor.
More particularly, the invention relates to a process for introducing fluidized solid particles into a bed of fluidised solids particles, for example for introducing catalyst particles into a fluidized bed of catalyst particles such as is present in the regenerator or reactor of a fluid catalytic cracking (FCC) reactor to rapidly attain uniform radial distribution of introduced solids, and to an apparatus therefor.
Fluidized catalytic cracking processes operate by circulating catalyst particles continuously from a reactor in which a hydrocarbon feed is cracked to lower boiling products, during which cracking carbonaceous material is deposited on the catalyst, via a regenerator in which the carbonaceous material is combusted to restore the catalyst activity, and returning catalyst particles to the reactor. Temperature of combustion in the regenerator is locally dependent on the amount of carbonaceous material on the catalyst and the supply of combustion gas in a given region.
Whilst operation with a single catalyst inlet opening at the regenerator side wall has for many years been satisfactory, the benefit to be obtained by improving radial distribution in conventional processes has become apparent. The benefits available from improved distribution of catalyst are particularly apparent for units comprising a regenerator vessel of increased diameter or in which regeneration is conducted at relatively high temperatures.
Such is the case for example with the processing of residual feeds or where limited elevation space or specific operation mode require operation with a reduced regenerator fluid bed height, combined with a large bed diameter. A condition for optimum regeneration is that the time for radial mixing of catalyst be less than that for coke combustion. With relatively high regeneration temperatures and heavier feed processing the rate of coke combustion is increased, requiring decrease in radial mixing time. With increase in diameter of a fluid bed, catalyst distribution must be more effective to prevent corresponding increase in radial mixing time. Should this condition not be met, radial gradients of coke, combustion gas and temperature form within the bed leading to an increase in oxygen content of flue gas and afterburn and a decrease in coke burning capacity for a given air blower.
In US Patent No. 4,595,567, devices disclosed for distributing catalyst into an FCC regenerator bed, described as air/catalyst distribution grids, would seem to comprise a plurality of openings 1.5 along the length of sections of a radially extending grid.
In US Patent No. 4,150,090 a device is disclosed comprising an axially located transport riser projecting from the lower part of an FCC regenerator vessel and supporting a plurality of radially extending fluidised catalyst distributor troughs, located in downward sloping direction at the surface of a regenerator bed.
Catalyst is transported and expelled along the length of the open-top troughs by means of fluidising gas supplied via conduits running along the length of the troughs and having apertures along the length thereof.
In US Patent No. 5,156,817 devices are disclosed for supplying catalyst to one or a plurality of open-sided channels defined between a base and top member of, for instance, inverted v-shaped cross-section by which means catalyst is discharged along the length of the channel(s), the channels) being closed at their proximal end. A single channel forms an incomplete annulus in an FCC regenerator bed. A plurality of channels are of different lengths and emanate in a fan formation from a supply conduit located towards the side of the bed, the longest channel extending to the axis of the regenerator bed.
2121fi~0 These devices suffer from the disadvantage that with normal operation, catalyst discharge is uneven along the distribution length, i.e. the plural openings, troughs and channels respectively, occurring to a lesser extent at the remote ends of the distribution lengths. The performance may be improved by employing excessive pressure drop which could be detrimental to the pressure balance of the unit. Provision of aeration conduits along distribution troughs incur high installation and maintenance costs.
In the latter cases radial mixing is governed by interaction between the flow pattern in the channels or troughs and the fluidised bed, and is therefor sensitive to changes in flow rate in the distributor which may affect the quality of radial distribution.
We have now found that fluids introduction and subsequent mixing into a fluid mass can be attained in a simple and controllable manner which is moreover robust to changes in distributor fluid flow. This manner relies on discharging the fluid at specific points in the fluid mass whilst avoiding interaction between the bed and the fluid to be distributed until the discharge point is reached. It has surprisingly been found that by this manner radial catalyst distribution gradients in the fluid mass are rapidly dissipated which would not have been expected. At the fluid discharge point the fluid kinetic energy may be locally eliminated after which the normal mixing action of the fluid mass promotes further radial mixing.
Accordingly, the present invention provides a process for radial distribution of fluid in a fluid mass wherein fluid is radially conveyed within and isolated from the fluid mass and discharged via a plurality of distribution points located radially in the fluid mass.
Suitably fluid is conveyed along radial paths, each path leading to a single distribution point, which point may provide one or more sites for contact of conveyed fluid and the fluids mass.
In a preferred embodiment of the process according to the invention fluid is discharged at a distance at least one quarter of 2~21~~~
the radius of the fluid mass from the fluid mass axis, more preferably at a distance of at least 4/10 of the radius, for example substantially one half of the radius.
Preferably kinetic energy is dissipated by impact or expansion of the fluid to be distributed.
The term "fluid" is herein used with reference to liquid, gas, slurry suspension of solids in fluid or to a mixture of fluidising gas and finely divided solids maintained in a fluidised form by the fluidising gas. Suitably the fluid comprises catalyst particles or reactive or combustible matter, such as fuel oil, shale oil or coke. Preferably the fluid comprises fluidised solids such as fluidised cracking catalyst particles.
The term "fluid mass" is used herein with reference to the contents of a vessel into which fluid is discharged in accordance with the present invention. Such a vessel may be of any cross-sectional geometry, such as circular, square, and is preferably circular. Fluid masses of any dimension may benefit from the present invention, for example masses of up to 20m or more in greatest diameter. Suitably a fluid mass is a gas or liquid to be treated or reacted, or is slurried or fluidised solids comprising catalyst or reactant, which may therefore be of relatively small or large radial cross-sectional area depending on the nature of fluids, into which mass fluid may be introduced periodically or continuously and retained for a sufficient residence time to allow necessary contact for treating or reaction. Suitably the fluid mass is in motion, whereby fluctuations in local velocity give a dispersive effect. Preferably the fluid bed comprises the reactor, stripper or regenerator bed of a fluid catalytic cracking unit into which catalytic cracking particles having entrained product gases or bearing carbonaceous deposits from cracking reactions are introduced for reaction, removal of product gases or combustion of deposits.
Suitably a fluid comprising finely divided solids particles is transported in lean or dense, preferably in lean phase.
-S-The term "radially" is used herein with reference to true radii or radial planes about the axis of the fluid mass or about a single fluid inlet location from which fluid is conveyed to distribution points.
The term "distribution point" is herein used with reference to a substantially localised distribution area, suitably 30 to 300$ of the cross-section of a radially conveyed fluid stream, which may provide one or more sites for contact of fluid and fluid mass.
According to a further embodiment of the present invention there is provided an apparatus for radial distribution of fluid into a fluid mass comprising a fluid supply conduit having a plurality of fluid conveying arms extending radially into the fluid mass characterised in that the arms have an enclosed length and one or more outlet openings at or near the end remote from the fluid conduit.
An apparatus according to the invention may additionally have an outlet opening located on the fluid conduit.
Suitably an apparatus according to the invention comprises fluid conveying arms of length of at least one quarter of the radius of the fluid mass, for example at lest 4/10 of the radius, or substantially one half of the radius.
An apparatus according to the invention may additionally comprise means at the outlet openings for dissipation of the kinetic energy of the fluid to be distributed.
~5 Preferably means for dissipating the fluid kinetic energy are impact or expansion means. The term "impact means" is herein used with reference to means provided in cooperation with the outlet opening whereby the fluid exiting the outlet opening impacts thereon, and is for example an impact face located in the fluid 30 stream path. Examples of impact means include splash plates and impact baffles which provide an impact face or faces to the distributed fluid. The term "expansion means" is herein used with reference to means for expanding the fluid volume, for example fluid conveying arms of increasing cross-sectional area in radial 35 direction or fluid-permeable packing provided at or downstream of the distribution point. Guide means such as ridges or channels may be provided on the fluid conveying arm walls to assist in expansion of the fluid stream.
Suitably impact means are supported on the fluid conveying arm or on the regenerator wall. Splash plates and impact baffles are arranged at such an angle to the fluids stream that an impact surface is presented to the fluids stream thereby dissipating the stream flow momentum and kinetic energy.
Suitable angle of impact surface to fluid stream flow direction depends on the density and velocity of the stream. In particular, impact means may be arranged at an angle of 90 to 165 degrees to the stream flow.
Fluid may be distributed from an opening towards the end of a fluid conveying arm, for example in the base or side thereof whereby the arm has a closed remote end, or from an opening in the remote end wall of a fluid conveying arm whereby it is clear that the arm is enclosed along the complete length.
In a particularly preferred embodiment of the invention a fluid conveying arm has an opening towards the end and in the base or side thereof. Optionally a splash plate is located beneath an opening in the base. This apparatus provides particularly good fluid dispersion. It is of particular advantage for distribution of fluidised catalyst in the lower part of a catalyst bed of a catalytic cracking catalyst regenerator that a splash plate prevents catalyst penetrating to the lower part of the bed and causing erosion of fluidising internals by impact thereon.
Impact means may 'be mono or multiplanar or may be of pyramidal configuration or even comprise a curved face or faces providing a gradually lessening degree of impact. Faces of a multiplanar impact means are directed away from each other.
Suitably expansion means comprise known fluid expander configurations located at or integral with the outlet of the fluid conveying arms. Hence an arm configuration providing an increasing cross sectional area in radial direction rnay be envisaged. The arm outlets may be somewhat horizontally elongate in cross section to z~z~s7~
_,_ limit the vertical dispersion of fluid. Expansion may also be achieved by means of structured fluid-permeable packing located at a fluid distribution point.
The supply conduit may be wholly or partially located in the :5 fluid mass. Preferably the supply conduit is substantially vertically arranged in the fluid mass and is more preferably a downflow or a riser conduit. Preferably the conduit is located substantially coaxially with the fluid mass but may be acentrically located in such a manner that the distributor arm outlets are regularly arranged in the fluid mass to ensure radial uniformity of outlet. A plurality of apparatus according to the invention may be arranged within a fluid mass for distribution of one or more fluids, and may be coaxially or acentrically arranged within the mass, or may comprise a primary apparatus axially located in the mass for optimum radial distribution and one or more secondary apparatus acentrically located in the mass for partial radial distribution or dispersion. A supply conduit which is located partially within the fluid mass suitably projects axially within a fluid containing vessel through the base thereof and is supplied by an external fluid conveying standpipe. A supply conduit which is located wholly within the fluid mass may be supplied by a fluid conveying standpipe which suitably projects within the fluid vessel via its sidewall to the lower part of the fluid bed. In an alternative embodiment. the conduit may be fed by a coaxially surrounding downer entering the fluid containing vessel above the surface of the fluid mass.
For use with fluidised solids transport fluidising gas is suitably introduced at the base of the supply conduit. Preferred transport gases are inert such as steam or air. Transport gas superficial velocity is sufficient to lift the solids in the riser, without causing flow segregation. Suitably gas superficial velocity for transporting fluidised cracking catalyst is 1 to 25m/s, preferably 3 to 12m/s. By control of the supply of the fluidising gas and of the solids, the fluidised solids flow in the riser is controlled. Suitably the riser solids flue: is maintained in the _8_ range of 200 to 3000, preferably in the range of 600 to 1500kg/m2/s.
The apparatus of the invention comprise a plurality of fluid conveying arms extending radially into the fluid mass. It will be understood that arms may extend substantially in a true radius in a cross-sectional plane of the fluid mass, or in a radial plane, i.e.
at an angle to the cross-sectional plane, suitably at an angle of up to 60 degrees. Preferably the number of arms is suited to give optimum distribution for an acceptable mechanical burden on the device. Preferably the device of the invention comprises 2 to 10 arms, more preferably 3 to 8, for example 4 arms. The arms may be of the same or different length and are preferably of the same length. Arms may be any desired shape in cross-section but preference is given to continuous non-angular cross-sectional f5 profiles.
For use with fluidised solids, control of fluids stream velocity in the fluid conveying arms minimises deposit of solids from the stream. Suitably, fluids stream velocity in the arms is maintained above a suitable minimum velocity, suitably greater than 3m/s, 2,0 preferably greater than 6m/s.
Suitably the fluids supply conduit comprises at its head a junction from which the fluid conveying arms radially extend. In a preferred embodiment of the device of the invention an axial riser or downflow conduit comprises a device to uniformly divide the 25 solids flow into the arms. Suitable devices include known riser top geometries, for example a blinded T-bend optionally in combination with guide vanes. Most preferred is a device comprising an inverted cone wherein the solids flow impinges centrally on the apex of the cone and is radially diverted with equal distribution into the 30 distributor arms. Suitably internal guide vanes project from the cone into the junction area for improved flow dispersion. This latter device has the advantage that pressure drop, resulting from change of solids stream directional momentum is considerably reduced, thereby reducing attrition of fluidised solids and erosion 35 of the distributor device.
8a The invention may be summarized as an apparatus for radial distribution of fluid into a fluid mass contained in a vessel comprising (a) a vessel containing a fluid mass;
(b) disposed within said vessel and within said fluid mass, 5. a centrally disposed fluid riser inlet conduit extending through a wall or floor of said vessel and oriented substantially vertically along the fluid riser inlet conduit's longitudinal axis, said riser inlet conduit having a plurality of fluid conveying arms each of said arms having an end remote from said fluid riser inlet conduit, and each of said arms extending radially and substantially horizontally outward from the vertical axis of said fluid riser inlet conduit and extending radially into the fluid mass wherein the arms have an enclosed length and (c) having along said enclosed length one or more outlet openings at or near the end remote from the fluid riser inlet conduit.
_ g _ The invention will now be illustrated by means of non-limiting example with reference to figures 1 to 5 in which Figure 1 is a plane view of a radial arm distributor located in a fluid mass containing vessel;
Figure 2 is a lengthwise cross-sectional view of a fluid distributor apparatus having splash plates located below the arms (two shown);
Figure 3 is a view of a riser head junction with guide vanes;
Figure 4 is a cross-section along line X - X of figure 2 1~ showing the splash plate mounting; , Figure S is a side section of a regenerator vessel of a fluid catalytic cracking unit comprising a catalyst distributor apparatus according to the invention.
A fluids distribution apparatus as shown in plane view figure 1 is preferably located in a fluid mass containing vessel (1) of circular cross-section.The distributor apparatus comprises a junction (2) of a supply conduit (not shown) for introduction of fluid into the vessel, from which fluid conveying arms (3,4,5,6) emanate in radial direction. In this embodiment four arms are shown, each illustrating one of alternative embodiments of arm outlet opening configurations. Arm (3) is open at the remote end (3a), allowing fluid outlet through the open end. Arm (4) comprises opening outlets (4a) in the side walls thereof at the remote end.
Arm (5) comprises an outlet opening (5a) in the base thereof. Arm (6) is of increased cross-sectional area at the remote end, allowing fluid outlet through the open end (6a). Impact means which are optionally associated with outlet openings of arms (3,4,5,6) are not shown. Fluid conveying arm (6) provides means for expansion of the fluid stream in the form of the increased cross-section arm 3U end (6a). A fluid withdrawal opening in the base of the vessel is shown (7) for removal of fluid from the vessel (1). The opening is preferably located at the site of least disturbance of distributed fluid.
The process according to the present invention using the fluids distribution apparatus shown in figure 1 is normally carried out as follows. Fluid is introduced into the fluid containing vessel via an enclosed conduit and is divided into streams at junction (2), for radial transport within but isolated from the fluid mass to distribution points of which four embodiments are illustrated (3a, 4a, 5a, 6a). Fluid outlet at the distribution points is shown by respective arrows (arrow not shown on arm (5)).
Once discharged the fluid comes into contact with the fluid mass and is further distributed by the action of the mass. Radially uniform distribution of incoming fluid has been found to occur by transporting fluid to discrete distribution points prior to contacting with fluid mass. Disruption of radial distribution by withdrawal of fluid from the vessel (1) is minimised by careful location of the withdrawal opening (7).
A fluids distribution apparatus shown in figure 2 comprises a riser inlet conduit (10) having at its head a junction (2) from which a plurality of arms (5) of which two are shown, emanate radially. Arms (5) comprise fluids outlet opening (5a) in the base thereof, in which opening a splash plate (8) is supported for improved radial fluid dispersion. Junction (2) includes an inverted cone (9) having internal guide vanes (not shown) for division of the fluids stream among the fluid conveying arms.
The process according to the present invention using the fluids distribution apparatus shown in figure 2 is normally carried out as follows. Fluid is introduced into the fluid containing 2'i vessel via enclosed conduit (10) and is separated at the conduit head by junction (2) and conveyed to fluid distribution points (5a) via enclosed fluid conveying arms (5). Fluid is discharged at distribution points (5a) and impacts on splash plates (8) with dissipation of fluid kinetic energy thereby allowing distribution by interaction with the fluid mass. Dune formation and erosion are minimised by provision of sloping arm mouth sections adjacent the riser.
An inverted cone .fluids stream divider is shown in figure 3 comprising a cap (11) with four guide vanes (12) located such that each space between the guide vanes is associated with the mouth of a fluid conveying arm.
The fluid conveying arm outlet opening of figure 2 as shown in figure 4 comprises a single opening (5a) in the base of the arm through which opening a splash plate having two impact faces (8) is suspended from a support member (14).
The regeneration vessel of a fluid catalytic cracking unit shown in figure 5 comprises a cylindrical vessel (16) provided with a riser inlet conduit (10) for introduction of fluid catalytic cracking catalyst into the fluidised catalyst bed (15). Fluidising gas is introduced at the base of conduit (10). The inlet conduit comprises a fluidised catalyst distributor device at junction (2) having fluid conveying arms (17) with outlet openings (17a). A
catalyst withdrawal opening (7) is shown in the base of the vessel.
Fluidisation nozzles are shown (18) for maintaining the catalyst bed in fluidised state.
The process according to the present invention, for example using the fluidised catalyst distribution apparatus shown in figure 5, is normally carried out as follows. Fluidised catalytic cracking catalyst is introduced into the regenerator vessel (16) via riser inlet conduit (10) and transported by means of fluidising gas introduced (not shown) at the base of the riser, to junction (2).
Catalyst is transported along catalyst conveying arms (17) to distribution points (17a) located within the fluidised catalyst bed. Catalyst is rapidly radially distributed. The catalyst bed is maintained in fluidised state by means of gas introduced via nozzles (18) by which further catalyst distribution is obtained by means of the energy of the fluid present in the catalyst bed.
Preferably kinetic energy is dissipated by impact or expansion of the fluid to be distributed.
The term "fluid" is herein used with reference to liquid, gas, slurry suspension of solids in fluid or to a mixture of fluidising gas and finely divided solids maintained in a fluidised form by the fluidising gas. Suitably the fluid comprises catalyst particles or reactive or combustible matter, such as fuel oil, shale oil or coke. Preferably the fluid comprises fluidised solids such as fluidised cracking catalyst particles.
The term "fluid mass" is used herein with reference to the contents of a vessel into which fluid is discharged in accordance with the present invention. Such a vessel may be of any cross-sectional geometry, such as circular, square, and is preferably circular. Fluid masses of any dimension may benefit from the present invention, for example masses of up to 20m or more in greatest diameter. Suitably a fluid mass is a gas or liquid to be treated or reacted, or is slurried or fluidised solids comprising catalyst or reactant, which may therefore be of relatively small or large radial cross-sectional area depending on the nature of fluids, into which mass fluid may be introduced periodically or continuously and retained for a sufficient residence time to allow necessary contact for treating or reaction. Suitably the fluid mass is in motion, whereby fluctuations in local velocity give a dispersive effect. Preferably the fluid bed comprises the reactor, stripper or regenerator bed of a fluid catalytic cracking unit into which catalytic cracking particles having entrained product gases or bearing carbonaceous deposits from cracking reactions are introduced for reaction, removal of product gases or combustion of deposits.
Suitably a fluid comprising finely divided solids particles is transported in lean or dense, preferably in lean phase.
-S-The term "radially" is used herein with reference to true radii or radial planes about the axis of the fluid mass or about a single fluid inlet location from which fluid is conveyed to distribution points.
The term "distribution point" is herein used with reference to a substantially localised distribution area, suitably 30 to 300$ of the cross-section of a radially conveyed fluid stream, which may provide one or more sites for contact of fluid and fluid mass.
According to a further embodiment of the present invention there is provided an apparatus for radial distribution of fluid into a fluid mass comprising a fluid supply conduit having a plurality of fluid conveying arms extending radially into the fluid mass characterised in that the arms have an enclosed length and one or more outlet openings at or near the end remote from the fluid conduit.
An apparatus according to the invention may additionally have an outlet opening located on the fluid conduit.
Suitably an apparatus according to the invention comprises fluid conveying arms of length of at least one quarter of the radius of the fluid mass, for example at lest 4/10 of the radius, or substantially one half of the radius.
An apparatus according to the invention may additionally comprise means at the outlet openings for dissipation of the kinetic energy of the fluid to be distributed.
~5 Preferably means for dissipating the fluid kinetic energy are impact or expansion means. The term "impact means" is herein used with reference to means provided in cooperation with the outlet opening whereby the fluid exiting the outlet opening impacts thereon, and is for example an impact face located in the fluid 30 stream path. Examples of impact means include splash plates and impact baffles which provide an impact face or faces to the distributed fluid. The term "expansion means" is herein used with reference to means for expanding the fluid volume, for example fluid conveying arms of increasing cross-sectional area in radial 35 direction or fluid-permeable packing provided at or downstream of the distribution point. Guide means such as ridges or channels may be provided on the fluid conveying arm walls to assist in expansion of the fluid stream.
Suitably impact means are supported on the fluid conveying arm or on the regenerator wall. Splash plates and impact baffles are arranged at such an angle to the fluids stream that an impact surface is presented to the fluids stream thereby dissipating the stream flow momentum and kinetic energy.
Suitable angle of impact surface to fluid stream flow direction depends on the density and velocity of the stream. In particular, impact means may be arranged at an angle of 90 to 165 degrees to the stream flow.
Fluid may be distributed from an opening towards the end of a fluid conveying arm, for example in the base or side thereof whereby the arm has a closed remote end, or from an opening in the remote end wall of a fluid conveying arm whereby it is clear that the arm is enclosed along the complete length.
In a particularly preferred embodiment of the invention a fluid conveying arm has an opening towards the end and in the base or side thereof. Optionally a splash plate is located beneath an opening in the base. This apparatus provides particularly good fluid dispersion. It is of particular advantage for distribution of fluidised catalyst in the lower part of a catalyst bed of a catalytic cracking catalyst regenerator that a splash plate prevents catalyst penetrating to the lower part of the bed and causing erosion of fluidising internals by impact thereon.
Impact means may 'be mono or multiplanar or may be of pyramidal configuration or even comprise a curved face or faces providing a gradually lessening degree of impact. Faces of a multiplanar impact means are directed away from each other.
Suitably expansion means comprise known fluid expander configurations located at or integral with the outlet of the fluid conveying arms. Hence an arm configuration providing an increasing cross sectional area in radial direction rnay be envisaged. The arm outlets may be somewhat horizontally elongate in cross section to z~z~s7~
_,_ limit the vertical dispersion of fluid. Expansion may also be achieved by means of structured fluid-permeable packing located at a fluid distribution point.
The supply conduit may be wholly or partially located in the :5 fluid mass. Preferably the supply conduit is substantially vertically arranged in the fluid mass and is more preferably a downflow or a riser conduit. Preferably the conduit is located substantially coaxially with the fluid mass but may be acentrically located in such a manner that the distributor arm outlets are regularly arranged in the fluid mass to ensure radial uniformity of outlet. A plurality of apparatus according to the invention may be arranged within a fluid mass for distribution of one or more fluids, and may be coaxially or acentrically arranged within the mass, or may comprise a primary apparatus axially located in the mass for optimum radial distribution and one or more secondary apparatus acentrically located in the mass for partial radial distribution or dispersion. A supply conduit which is located partially within the fluid mass suitably projects axially within a fluid containing vessel through the base thereof and is supplied by an external fluid conveying standpipe. A supply conduit which is located wholly within the fluid mass may be supplied by a fluid conveying standpipe which suitably projects within the fluid vessel via its sidewall to the lower part of the fluid bed. In an alternative embodiment. the conduit may be fed by a coaxially surrounding downer entering the fluid containing vessel above the surface of the fluid mass.
For use with fluidised solids transport fluidising gas is suitably introduced at the base of the supply conduit. Preferred transport gases are inert such as steam or air. Transport gas superficial velocity is sufficient to lift the solids in the riser, without causing flow segregation. Suitably gas superficial velocity for transporting fluidised cracking catalyst is 1 to 25m/s, preferably 3 to 12m/s. By control of the supply of the fluidising gas and of the solids, the fluidised solids flow in the riser is controlled. Suitably the riser solids flue: is maintained in the _8_ range of 200 to 3000, preferably in the range of 600 to 1500kg/m2/s.
The apparatus of the invention comprise a plurality of fluid conveying arms extending radially into the fluid mass. It will be understood that arms may extend substantially in a true radius in a cross-sectional plane of the fluid mass, or in a radial plane, i.e.
at an angle to the cross-sectional plane, suitably at an angle of up to 60 degrees. Preferably the number of arms is suited to give optimum distribution for an acceptable mechanical burden on the device. Preferably the device of the invention comprises 2 to 10 arms, more preferably 3 to 8, for example 4 arms. The arms may be of the same or different length and are preferably of the same length. Arms may be any desired shape in cross-section but preference is given to continuous non-angular cross-sectional f5 profiles.
For use with fluidised solids, control of fluids stream velocity in the fluid conveying arms minimises deposit of solids from the stream. Suitably, fluids stream velocity in the arms is maintained above a suitable minimum velocity, suitably greater than 3m/s, 2,0 preferably greater than 6m/s.
Suitably the fluids supply conduit comprises at its head a junction from which the fluid conveying arms radially extend. In a preferred embodiment of the device of the invention an axial riser or downflow conduit comprises a device to uniformly divide the 25 solids flow into the arms. Suitable devices include known riser top geometries, for example a blinded T-bend optionally in combination with guide vanes. Most preferred is a device comprising an inverted cone wherein the solids flow impinges centrally on the apex of the cone and is radially diverted with equal distribution into the 30 distributor arms. Suitably internal guide vanes project from the cone into the junction area for improved flow dispersion. This latter device has the advantage that pressure drop, resulting from change of solids stream directional momentum is considerably reduced, thereby reducing attrition of fluidised solids and erosion 35 of the distributor device.
8a The invention may be summarized as an apparatus for radial distribution of fluid into a fluid mass contained in a vessel comprising (a) a vessel containing a fluid mass;
(b) disposed within said vessel and within said fluid mass, 5. a centrally disposed fluid riser inlet conduit extending through a wall or floor of said vessel and oriented substantially vertically along the fluid riser inlet conduit's longitudinal axis, said riser inlet conduit having a plurality of fluid conveying arms each of said arms having an end remote from said fluid riser inlet conduit, and each of said arms extending radially and substantially horizontally outward from the vertical axis of said fluid riser inlet conduit and extending radially into the fluid mass wherein the arms have an enclosed length and (c) having along said enclosed length one or more outlet openings at or near the end remote from the fluid riser inlet conduit.
_ g _ The invention will now be illustrated by means of non-limiting example with reference to figures 1 to 5 in which Figure 1 is a plane view of a radial arm distributor located in a fluid mass containing vessel;
Figure 2 is a lengthwise cross-sectional view of a fluid distributor apparatus having splash plates located below the arms (two shown);
Figure 3 is a view of a riser head junction with guide vanes;
Figure 4 is a cross-section along line X - X of figure 2 1~ showing the splash plate mounting; , Figure S is a side section of a regenerator vessel of a fluid catalytic cracking unit comprising a catalyst distributor apparatus according to the invention.
A fluids distribution apparatus as shown in plane view figure 1 is preferably located in a fluid mass containing vessel (1) of circular cross-section.The distributor apparatus comprises a junction (2) of a supply conduit (not shown) for introduction of fluid into the vessel, from which fluid conveying arms (3,4,5,6) emanate in radial direction. In this embodiment four arms are shown, each illustrating one of alternative embodiments of arm outlet opening configurations. Arm (3) is open at the remote end (3a), allowing fluid outlet through the open end. Arm (4) comprises opening outlets (4a) in the side walls thereof at the remote end.
Arm (5) comprises an outlet opening (5a) in the base thereof. Arm (6) is of increased cross-sectional area at the remote end, allowing fluid outlet through the open end (6a). Impact means which are optionally associated with outlet openings of arms (3,4,5,6) are not shown. Fluid conveying arm (6) provides means for expansion of the fluid stream in the form of the increased cross-section arm 3U end (6a). A fluid withdrawal opening in the base of the vessel is shown (7) for removal of fluid from the vessel (1). The opening is preferably located at the site of least disturbance of distributed fluid.
The process according to the present invention using the fluids distribution apparatus shown in figure 1 is normally carried out as follows. Fluid is introduced into the fluid containing vessel via an enclosed conduit and is divided into streams at junction (2), for radial transport within but isolated from the fluid mass to distribution points of which four embodiments are illustrated (3a, 4a, 5a, 6a). Fluid outlet at the distribution points is shown by respective arrows (arrow not shown on arm (5)).
Once discharged the fluid comes into contact with the fluid mass and is further distributed by the action of the mass. Radially uniform distribution of incoming fluid has been found to occur by transporting fluid to discrete distribution points prior to contacting with fluid mass. Disruption of radial distribution by withdrawal of fluid from the vessel (1) is minimised by careful location of the withdrawal opening (7).
A fluids distribution apparatus shown in figure 2 comprises a riser inlet conduit (10) having at its head a junction (2) from which a plurality of arms (5) of which two are shown, emanate radially. Arms (5) comprise fluids outlet opening (5a) in the base thereof, in which opening a splash plate (8) is supported for improved radial fluid dispersion. Junction (2) includes an inverted cone (9) having internal guide vanes (not shown) for division of the fluids stream among the fluid conveying arms.
The process according to the present invention using the fluids distribution apparatus shown in figure 2 is normally carried out as follows. Fluid is introduced into the fluid containing 2'i vessel via enclosed conduit (10) and is separated at the conduit head by junction (2) and conveyed to fluid distribution points (5a) via enclosed fluid conveying arms (5). Fluid is discharged at distribution points (5a) and impacts on splash plates (8) with dissipation of fluid kinetic energy thereby allowing distribution by interaction with the fluid mass. Dune formation and erosion are minimised by provision of sloping arm mouth sections adjacent the riser.
An inverted cone .fluids stream divider is shown in figure 3 comprising a cap (11) with four guide vanes (12) located such that each space between the guide vanes is associated with the mouth of a fluid conveying arm.
The fluid conveying arm outlet opening of figure 2 as shown in figure 4 comprises a single opening (5a) in the base of the arm through which opening a splash plate having two impact faces (8) is suspended from a support member (14).
The regeneration vessel of a fluid catalytic cracking unit shown in figure 5 comprises a cylindrical vessel (16) provided with a riser inlet conduit (10) for introduction of fluid catalytic cracking catalyst into the fluidised catalyst bed (15). Fluidising gas is introduced at the base of conduit (10). The inlet conduit comprises a fluidised catalyst distributor device at junction (2) having fluid conveying arms (17) with outlet openings (17a). A
catalyst withdrawal opening (7) is shown in the base of the vessel.
Fluidisation nozzles are shown (18) for maintaining the catalyst bed in fluidised state.
The process according to the present invention, for example using the fluidised catalyst distribution apparatus shown in figure 5, is normally carried out as follows. Fluidised catalytic cracking catalyst is introduced into the regenerator vessel (16) via riser inlet conduit (10) and transported by means of fluidising gas introduced (not shown) at the base of the riser, to junction (2).
Catalyst is transported along catalyst conveying arms (17) to distribution points (17a) located within the fluidised catalyst bed. Catalyst is rapidly radially distributed. The catalyst bed is maintained in fluidised state by means of gas introduced via nozzles (18) by which further catalyst distribution is obtained by means of the energy of the fluid present in the catalyst bed.
Claims (8)
1. An apparatus for radial distribution of fluid into a fluid mass contained in a vessel comprising (a) a vessel containing a fluid mass; (b) disposed within said vessel and within said fluid mass, a centrally disposed fluid riser inlet conduit extending through a wall or floor of said vessel and oriented substantially vertically along the fluid riser inlet conduit's longitudinal axis, said riser inlet conduit having a plurality of fluid conveying arms each of said arms having an end remote from said fluid riser inlet conduit, and each of said arms extending radially and substantially horizontally outward from the vertical axis of said fluid riser inlet conduit and extending radially into the fluid mass wherein the arms have an enclosed length and (c) having along said enclosed length one or more outlet openings at or near the end remote from the fluid riser inlet conduit.
2. The apparatus according to claim 1 wherein said fluid conveying arms have a length of at least one quarter of the radius of the fluid mass.
3. The apparatus according to claim 1 further comprising means for dissipating kinetic energy of the fluid as the fluid is discharged at each outlet opening.
4. The apparatus according to claim 3 wherein said kinetic energy dissipating means comprises impact or expansion means.
5. The apparatus according to claim 4 wherein said impact means include splash plates or impact baffles wherein said splash plates or impact baffles are integral to or fixedly attached to said fluid conveying arms.
6. The apparatus according to claim 4 wherein said expansion means include fluid conveying arms of increasing cross-sectional area in radial direction or fluid-permeable packing.
7. The apparatus according to claim 4 wherein the fluid conveying arms have an outlet opening in a base or side thereof whereby the arm has a closed remote end.
8. The apparatus according to claim 4 wherein the kinetic energy dissipating means consists essentially of expansion means and wherein the fluid conveying arms are enclosed along their complete length and have an outlet opening in the remote end wall.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP93201162 | 1993-04-21 | ||
| EP93201162.0 | 1993-04-21 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2121670A1 CA2121670A1 (en) | 1994-10-22 |
| CA2121670C true CA2121670C (en) | 2004-11-30 |
Family
ID=8213785
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002121670A Expired - Fee Related CA2121670C (en) | 1993-04-21 | 1994-04-19 | Process and apparatus for distributing fluids in a container |
Country Status (11)
| Country | Link |
|---|---|
| US (1) | US6221318B1 (en) |
| EP (1) | EP0622116B1 (en) |
| JP (1) | JPH0712470A (en) |
| KR (1) | KR100328587B1 (en) |
| CN (1) | CN1050531C (en) |
| AU (1) | AU673240B2 (en) |
| BR (1) | BR9401540A (en) |
| CA (1) | CA2121670C (en) |
| DE (1) | DE69406838T2 (en) |
| SG (1) | SG86288A1 (en) |
| TW (1) | TW351683B (en) |
Families Citing this family (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5773378A (en) * | 1996-10-30 | 1998-06-30 | The M. W. Kellogg Company | Spent catalyst distribution |
| RU2131764C1 (en) * | 1997-02-18 | 1999-06-20 | Акционерное общество "Салаватнефтеоргсинтез" | Methane converter mixer |
| US6503460B1 (en) * | 1999-03-17 | 2003-01-07 | Kellogg Brown & Root, Inc. | Staged catalyst regeneration in a baffled fluidized bed |
| US6797239B1 (en) * | 2000-11-22 | 2004-09-28 | Shell Oil Company | Spent catalyst distributor |
| DE60210330T2 (en) * | 2001-12-21 | 2006-08-24 | Shell Internationale Research Maatschappij B.V. | METHOD OF REGENERATING USED FCC CATALYST |
| US20060165605A1 (en) * | 2001-12-28 | 2006-07-27 | Ye-Mon Chen | Process to regenerate fcc spent catalyst |
| US7745365B2 (en) * | 2007-03-09 | 2010-06-29 | Stone & Webster Process Technology, Inc. | Bathtub-type spent catalyst distributor for effective counter-current regeneration in fluid catalytic cracking units |
| US8728302B2 (en) | 2010-06-25 | 2014-05-20 | Exxonmobil Research And Engineering Company | Spent catalyst riser distributor |
| CA2985195A1 (en) * | 2015-05-11 | 2016-11-17 | Shell Internationale Research Maatschappij B.V. | Fluidized solids distributor |
| FR3065886B1 (en) * | 2017-05-05 | 2021-12-31 | Ifp Energies Now | NEW DEVICE FOR DISTRIBUTION OF POLYPHASIC MIXTURE IN AN ENCLOSURE COMPRISING A FLUIDIZED MEDIUM |
| US10376856B2 (en) * | 2017-07-28 | 2019-08-13 | Uop Llc | Methods for fluid contacting in a downflow vessel |
| FR3082125B1 (en) | 2018-06-06 | 2021-05-21 | Ifp Energies Now | POLYPHASIC MIXING DISTRIBUTION DEVICE IN AN ENCLOSURE CONTAINING A FLUIDIZED MEDIUM |
| WO2023009031A1 (en) * | 2021-07-26 | 2023-02-02 | Акционерное общество "Специальное конструкторско-технологическое бюро "Катализатор" | Regenerator for a с3-с5 paraffin dehydrogenation system (variants) |
| CN113856426B (en) * | 2021-09-26 | 2025-07-29 | 普欧(上海)环保科技有限公司 | An exhaust gas treatment device |
| FR3144024B1 (en) | 2022-12-22 | 2025-07-04 | Ifp Energies Now | Fluidized bed distributor |
Family Cites Families (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2608474A (en) * | 1949-01-14 | 1952-08-26 | Shell Dev | Apparatus for contacting gaseous fluids with powdered solids |
| US2999012A (en) * | 1958-09-03 | 1961-09-05 | Sun Oil Co | Apparatus for contacting hydrocarbons with solids |
| FR1338537A (en) * | 1962-08-17 | 1963-09-27 | Siderurgie Fse Inst Rech | Fluidization device for powdery materials |
| GB1310886A (en) * | 1969-11-25 | 1973-03-21 | Coal Industry Patents Ltd | Apparatus for distributing particulate material |
| US3912460A (en) * | 1973-11-19 | 1975-10-14 | Texaco Development Corp | Method and article for distributing air in a regenerator |
| DE2707478A1 (en) | 1976-03-01 | 1977-09-08 | Pullman Inc | METHOD AND DEVICE FOR REGENERATING CRACK CATALYSTS |
| GB2069365B (en) * | 1980-02-19 | 1984-06-13 | Uop Inc | Catalyst regeneration process and apparatus |
| US4443551A (en) * | 1982-01-11 | 1984-04-17 | Texaco Inc. | Method and new distributor for delivering high velocity gas from a gas distributor through a nozzle with decreased erosion in the nozzle |
| FR2520634B1 (en) * | 1982-02-02 | 1987-02-13 | Inst Francais Du Petrole | METHOD AND DEVICE FOR SUPPORTING SOLID PARTICLES AND INTRODUCING A LIQUID LOAD TO THE BOTTOM OF A CONTACT AREA |
| FR2529905B1 (en) * | 1982-07-09 | 1988-04-08 | Inst Francais Du Petrole | PROCESS AND DEVICE FOR HYDROPROCESSING HYDROCARBONS IN LIQUID PHASE, IN THE PRESENCE OF A CATALYST IN EXPANDED OR BOILING BED |
| US4595567A (en) | 1984-12-28 | 1986-06-17 | Uop Inc. | Cooling fluidized catalytic cracking regeneration zones with heat pipe apparatus |
| US4664888A (en) * | 1985-06-27 | 1987-05-12 | Texaco Inc. | Fluid catalytic cracking catalyst-vapor separator |
| US5205993A (en) * | 1989-11-06 | 1993-04-27 | Mobil Oil Corporation | Catalytic cracking apparatus using cross-flow regenerator |
| US5156817A (en) | 1990-05-15 | 1992-10-20 | Exxon Research And Engineering Company | Fccu regenerator catalyst distribution system |
-
1994
- 1994-04-07 TW TW083103020A patent/TW351683B/en not_active IP Right Cessation
- 1994-04-19 BR BR9401540A patent/BR9401540A/en not_active IP Right Cessation
- 1994-04-19 DE DE69406838T patent/DE69406838T2/en not_active Expired - Lifetime
- 1994-04-19 AU AU60564/94A patent/AU673240B2/en not_active Ceased
- 1994-04-19 JP JP6103228A patent/JPH0712470A/en active Pending
- 1994-04-19 EP EP94201077A patent/EP0622116B1/en not_active Expired - Lifetime
- 1994-04-19 SG SG9601739A patent/SG86288A1/en unknown
- 1994-04-19 CA CA002121670A patent/CA2121670C/en not_active Expired - Fee Related
- 1994-04-20 CN CN94104295A patent/CN1050531C/en not_active Expired - Lifetime
- 1994-04-20 KR KR1019940008525A patent/KR100328587B1/en not_active Expired - Fee Related
- 1994-04-20 US US08/230,173 patent/US6221318B1/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| CA2121670A1 (en) | 1994-10-22 |
| AU6056494A (en) | 1994-10-27 |
| DE69406838T2 (en) | 1998-04-02 |
| CN1094656A (en) | 1994-11-09 |
| DE69406838D1 (en) | 1998-01-02 |
| CN1050531C (en) | 2000-03-22 |
| US6221318B1 (en) | 2001-04-24 |
| BR9401540A (en) | 1994-11-22 |
| JPH0712470A (en) | 1995-01-17 |
| KR100328587B1 (en) | 2002-07-27 |
| EP0622116A1 (en) | 1994-11-02 |
| SG86288A1 (en) | 2002-02-19 |
| EP0622116B1 (en) | 1997-11-19 |
| TW351683B (en) | 1999-02-01 |
| AU673240B2 (en) | 1996-10-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2121670C (en) | Process and apparatus for distributing fluids in a container | |
| KR101274902B1 (en) | Catalytic Regeneration Apparatus and Method | |
| US4514285A (en) | Catalytic cracking system | |
| RU2449003C2 (en) | Device and method for catalytic cracking | |
| EP1352038B1 (en) | Spent catalyst distributor | |
| AU2002229564A1 (en) | Spent Catalyst Distributor | |
| US6146519A (en) | Gas solid contact riser with redistribution | |
| US7316733B1 (en) | Diffuser for separator vessel | |
| US4289729A (en) | Biased degasser for fluidized bed outlet | |
| US5015363A (en) | FCC stripping method | |
| US3607730A (en) | Apparatus and method for conversion of hydrocarbons | |
| US5098553A (en) | Catalytic cracking process using regenerator with multiple catalyst outlets | |
| US20060165605A1 (en) | Process to regenerate fcc spent catalyst | |
| US5062944A (en) | Catalytic cracking process with multiple catalyst outlets | |
| EP1456325B1 (en) | Process to regenerate spent fcc catalyst | |
| US4927606A (en) | FCC Stripping apparatus | |
| US2766186A (en) | Conversion of fluid hydrocarbon in the presence of a moving mass of granular catalyst | |
| US2978279A (en) | Method and apparatus for transferring contact material | |
| CN114026206B (en) | Riser extension apparatus and method | |
| US2652317A (en) | Reactor inlet | |
| KR20240027031A (en) | Chemical processing vessel with plate grid distributor and method of operating the same | |
| EP0129621B1 (en) | Apparatus and process for fluidized catalytic cracking of hydrocarbons and catalyst regeneration | |
| US2701185A (en) | Apparatus for regeneration of solid contact material | |
| US2849380A (en) | Method and apparatus for catalytic conversion of liquid feeds | |
| AU626121B2 (en) | Side-to-side fcc stripping apparatus with baffle-skirts having stripping gas injection ports |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| MKLA | Lapsed |
Effective date: 20140422 |